Antitack agent



5ml El STEAM TANK.

TANL

ecYcLa) M1\..L.. Ema/Avon f- S'rmppms EJ Ecran.

SHaEDDmG FLASHED i ADDmoN j il AGEN-rs WATELV MALL- UP To. Ae 1N LD QE Ln.- YE un. i e fu O ro. e m m L w m G. R. SCOTT AN'IITACK AGENT Filed July 19. 1947 FLASH TANK 12E/erom lzCoNv avon.

L mso@ s ,TM L m o. WSS MLU v ma 7+ A... O. Lm n. am nr N s C I. H ws mwN 5 u mn AV- ODL OW! CGA n ,.w.

Sept. 23, 1952 FEED T CATALYs-r y .|uroMA1lc.

Grady 12. Scott, A

/lw f.. L mi jat low temperature. Ynature of certain of the reactants' the slurry is .discharged into a welleagitated body of aheated Patented Sept. 23,1952

vStandard Ol Develop ment Company, a corpo- Application July-19, 1947, serial No. 762,189

This invention relates to esses and apparatusand-particularly toprocesses .and apparatus for= the low. temperature p olymerizaticn of iso-olens -diolefins or mixturesy of so-olefins and Certain preferred-details of theprocess ap'- paratus will be apparent andthe invention itself will vbe best understood byxrefer'ence to thezfollowing specification and accompanying drawing-.- It'has beenrknownfor some time that high molecular Weight polymers, yi. el', having a molecular weight of from aboutif15,00025,000 upto 300,000or more (as determinedbythe Staudinger method) are obtained if .iso-olens," such,` as isobutylene, are contacted with Friedel-Crafts type catalyst such as aluminum chloride and the like at temperatures .belovv about .-10" F. (See, for example,'Mueller-Cunradi` U. S.' PatentNo. 2,203,873, issued June 11, 1940.) More recently it Was found that a copolymer which is curable with sulfur is obtained if a'mixture of about '70 toi/99.5 Weight percent of an iso-olenvsuch'f as isobutyltures. 1 These polymerizations have been con- .ducted in the presence of an internal refrigerant such as liquefied ethylene, inv which case the heat of reaction is removed directly vby evaporation of part of the ethylene Without the necessity for transferring heatthrough the surfaces of the reyactionvessels or through cooling coils arranged in the reaction vessels, or in the presence of large quantities-of a diluent such *as methyl chloride, cooled by external means. Consequently, thereaction is now carried out in such a manner as to b e claims.. (o1. aco-#zati polymerization procfl tained at a ltemperature well above the boiling Dontofthe majority ofthe volatilematerials accompanyingthe polymer, to form a slurryof -nelyvdivided polymer: particleszin the'` warm keep the solid polymer particles in a finely divided condition suspended in the cold reaction mixture so that a slurry Vof solid polymer in the cold 'reaction'mixture is obtained which can be handled In view of the inflammable liquid medium, such as Water, which may be designated as the ashing medium in which Ythe polymer is suitably insoluble and which is mainliquid and to ash off the reaction mixture.- 'I'his slurrylis thenstripped of anypresidual volatile materials and dried while being carried through a tunnel on aV screen or on sections of, a perforated plate in thepresence of warmfair. A It 4has Yalso been lthe practice to coat theonveyorsurfaces with agents such :ias .zino stearate, zine oxide,

aqueous soap solutioma soap .of an alkaline earth metal, talc, clays, castor oil, corn loilands'imilar materials, in order to alleviate the. problemfof the polymer sticking to the dryer surfaces.

-This is a particularly'critical problem with regard to, these' typesof polymers 'sincethey exhibit far greater sticking abilities than the usual :type of synthetic rubbers. For example, the folvlowing comparative'data on the relative stickiness of uncompounded polymers produced by the above process and those produced by copolymerizing butadiene With styrene. f

l.Contact time seconds under force of 2.65 lbs.

It Will be noted that by sticking fresh .out s .faces of the copolymer of isoprene and isobutyl- Aene together with 95.8% of the original raw strength is obtained While only 16.4% is obtained for the copolymer of butadiene and styrene. This indicates that the copolymer of isoprene and isdbutylene is far stickier than the copolymerof ,butadiene and styrene and' therefore it is rmore vdifcultto prevent the copolymer of isoprene and vabove 220 F., and when the dryer temperature is kept low enough to prevent fusion, the polymer is often inadequately dried. Above its lmelting point, however, zinc stearate loses much of' its anti-sticking eiect against iso-olenic polymers.

The use of dry talc or clays is not usually satisfactory because the dry pigments are not sufficiently adherent to the dry screen to be serviceable under the conditions of use. If wetted or applied as a slurry, pigments such as zinc oxide, talc and clays form coatings which either become powdery and flaky upon drying with the result that such coatings are largely removed from the screen upon contact With the polymers or Which web over and plug the perforations or screen openings in the conveyor, thus interfering with the circulation of air through the bed of polymer. Y

It is, therefore, the principal object of this invention to provide a method of removing volatile impurities from polymers Which will permit more efficient operation of process vand prevent sticking of the polymers to the heated surfaces of the apparatus.

A further object of this invention is to provide a coating which will not readily be removed completely.` from the metal surfaces' by polymers, Which-does notappreciablyiaiiect polymer quality and which will permit drying the'polymerat tem- These and, other. objects .of this invention are accomplished bypass`ing the polymer through a 'heating zone, the1polymer-contacting'surfaces or fwhich. are fcoatedmith an emulsion of a low vapor pressure'fatty oil, andan emulsifying agent.

order to make the. invention more clearly understood, there is shoivn'in -the accompanying drawing one `means for carrying the same into practical effect.

Referring, therefore, to'the drawing, there is shown aireactor I! wherein iso-.olenic materials and preferably mixtures of iso-oleiinic 'and diolenic materials alone' or together with a diluent supplied `throughfeed inlet .2 yare reacted at low terriperatures,preferably.` around 440 by the vapor. The liashed gases are withdrawn from the flash tank through line i5 and are passed to suitable puriiication and recovery means for reconditioning the flashed materials for reuse in the process.

The Water or other liquid :medium is heated, as

lby the introduction of steam thereinto, and

vigorously agitated by means of suitable Astirrers .or the like to .keep the polymer suspended as a uniform slurry in the liquid. Liquid may lalso bewithdravvn fromthe hash tank 'through line l'I and .pumped vback into the flash tank as at 8 in such .a manner 'as to impinge against the polymer stream entering the ash tank thereby breaking it up in order to prevent agglomeration of the polymer Yinto relatively large masses which might plug .the water slurry systemI and whichmig'ht 'contain excessive "amc'nunts of trapped volatile liquid.

AThe polymeri's Withdrawn from. the ilash tank through line '9 .as `a slurry of iinely divided solid particles suspended in the Warm liquid and is discharged into the stripping tank IB. The treatment of the polymer as a slurry in the Warm iiuid,

4 if necessary with injection of stripping vapors such as steam, is carried out to such a degree that nearly all the highly volatile materials originally absorbed in or adsorbed on the polymer and dissolved in the liquid are removed. A preferred type of operation is one in which the volatiles are removed in two zones, the iirst, as in flash tank 5 at atmospheric or slightly above atmospheric `pressure and the other "as vin stripping tank S0 at below atmospheric pressure. Preferably, the Water in the stripper IQ is boiling, due to use of vacuum. The ovv of Water is usually so large that steam does not have to be added y' to the stripper when the Water enters hot enough.

pending liquid, itis discharged into a. deivatering press l2'of theendless screengtype `wherein it'is passed betweenpressure rollers which squeeze out furtherv amounts of. yWater or `'suspending liquid. The water or the like passing through the vibrating screen is .desirably collected, make-up liquid and any A.desi-'red addition agents, fsuch as alkalies for reducing acidi-tyv caused byV decomposition of the catalyst, zinc stearato, .dieper-sing agents, etc; are added;fvvhereup'orlY the liquid is recycled-'to the flashtank through line i3. The liquid removed .in` the press 1.2 may be discharged to the sewer or recovered in suitable fashion.;

The polymer is then discl'iarged into a suitable disintegrating means such as a hammer mill 4 in order to .reduce the size of the polymer particles preparatory -to discharge into the dryer system. The polymer particles discharged from the hammer mill areconveyed by suitable means such as an elevator i5 to an oscillating-feeder 16 `which serves to distribute the polymer on the conveyor `screen irpassing through the dryer I8.

The polymer is passedfrom the endless dryer conveyor 'il to conveying means iIS for carrying itto the-compressing means. In the case where the material is discharged from the dryer in the form of a blanket, a large'automatic shear .2li may be providedl to cuti't into small. easily handled pieces or av set of tearing rolls or some .other mechanical shredder can be used..

The compressing 'of the ypolymer maypbjeeffected by passing it once or several times through a hot-or cold rubber mill to-,give'arelatively compact and smooth sheet which may be cut and 4stacked or 'folded into a suitable container, or

alternatively, it may be extruded and then pack-` aged in the same Way or it may .even be baled directly as it cornes from the dryer. If small traces of moisture still remain in the material leaving the dryer (as, for example, after drying soft stocks), itis possible to remove this water `expeditiously and with a minimum of mechanical breakdown by hot extrusion followed by batch or `continuous milling into a suitable sheet. lInvthe drawing, mills 2l and 22 are shown in which'the polymermay be subjected to continuous milling in two stages. V.An extruder 23 Which may also, if desired, be provided with a steam jacket 24 may be used for compressing the polymer. With the arrangement shown, the polymer .may be milled or extruded-or both as desired.

Another purpose of this compressing `step in this sequence of'i'lnishing operations is to put the rpolymer into a form .having a minimum of surface exposed to the air. The deterioration of the polymer which takes place very slowly'during storage even under the best of conditions is known to occur principally atthe surface ofthe material where exposed to the air and, yby Yde creasing the surface area of a given amount of A ypolymer by compacting it, the rate of deterioration is markedly decreased. Also, after proper packaging, the container further reduces the eX`- posure to air and consequent deterioration. The packaging of the compressed polymer is conveniently effected by passing the sheeted polymer from the mill or extruder into a suitable cooler 25 wherein it is cooled to about 160 F. or below and preferably to about room temperature, whereupon it is passed to the cutting and stacking machine 26 and placed in suitable containers as at 21. According to the invention, polymer fro which the major quantity of liquid has been re moved by pressing, etc., is treated in the dryer under conditions to remove the residual adhering or occluded fluid, usually water, as well as traces of impurities or oy-products of relatively low volatility carried through with the polymer from the reaction zone. The drying'or removalof the aforesaid `V'impurities orby-products is veffected vwithout subjecting the polymer to temperatures or mechanical treatment sufficient tol materially degrade the physical properties of the polymer and without initiating chemical reactions which would induce deterioration ofY the product in storage. For this purpose, it may be desirable to have a small amount of a stabilizer present-such as phenylbetanaphthylamine. Removal of` substantially all of the water and Vvolatile impurities Ais essential since appreciable amounts thereof usually interfere with proper processingvoffthe uncured polymers or tend' to cause blistering during curing of articles whichlare subsequently fabricated from the polymer; I f

The dryer used may be avcontinuous conveyor dryer, the polymer being 'carried `through la tunnel on a screen or on Vsections of perforated plate, although other types of dryers maybe usedl v'-lhe dryer is preferably of a'tunnel-,icontinuousconveyor, through-flowrtype ofeither'one or-more passes, wherein a 'considerable zfl'owlf air or other inert gas is recirculated over steam coils'o'r other heating elements and through or agains'tthe'bed of polymer material slowly moving through the dryer on a perforated conveyor belt or'scr'een. The preferred drying temperature is'usuallybetween 200 F. and 350 F; and is dependent upon the molecular weight ofiA the .polymre being handled and the vtime of exposure'tosaidI 'drying temperature. It is desirable, wherefp'ossible, to avoid softening the polymer in the dryeriby too long exposure to high temperatures so a'sto-permit better circulation of air' throughthe'" bed. However, with some products,"softening'v takes place quite readily and in these cases'the "avoidI` ance of softeningwould'limit temperaturesto a degree which gives "very slow. drying rates. l In such cases, it is usually more effective to accept the softening and the consequent low air 'rate through the bed and'to operate at'considerably higher temperatures, limited by the tendency of the polymer vto adhere to the perforated vplates or by thedanger of deteriorating theproduct quality. For rapid conveyor speeds, i.\ e.,.sliort residence times in the dryer, higher drying temperatures can be used than for slow. .conveyo speeds. Polymers such as polyiso-olens and copoly- Vmers of iso-olens with diolens prepared at low ..6 temperatures in the-presence of Friedel-Crafts type catalysts tend' slowly to undergo'a reduction in molecular weight and a deterioration in physical properties upon prolonged exposure to air at temperatures even 'as low'asy 200 F. Also, polymerslof the lower molecular weight ranges tend. to fuse when subjected to temperatures in the drying Arange for appreciable lengths of' time, tending to decrease the'bed thickness and size of'voids in the layer of 'materialen the'conveyor an'dcausing the polymerto stick to the conveyor, thus decreasing the air flow,'increasing the necessary drying time and generally decreasing the e'iciency of operation. With medium or low molecular weight stocks, softening may occur so readily that'drying rates are very poor if the temperature'lis maintained low enough to avoid softening. Although higher temperatures give low or almost no air flow through'the bed, the corresponding high vapor pressure and diffusion aids the drying so that -it frequently pays to run the dryer'as hot as possible. -In many'cases, therefore,the latter portion of thedryer -will operate mainly as an imp inge'inent or crossacirculation dryer due to softening and coalescence of the`polyme'r on the dryer belt. In such cases the practical limit on the temperature in the dryer, aside fromv oxidation or breakdown of the polymer is set by the tendency of the product to stick to the yscreen or dryer plates;

' I As pointed out above,-it has been attempted to overcome'this problem of sticking by coating the conveyor surfaces with a suitable anti-sticking agent butnone of the prior materials have been 'sufficiently satisfactory to allow the temperature to be materially increased without" requiring fre# quent interruptions for cleaning the surfaces. According` to the present-,invention much higher temperatures can be' reached Vand more satisfactory operation canbe obtained, from the standpointfof capacity as well as eliminating fouling of the equipment, by the use of non-volatile fatty oil-water lemulsion andan emulsifying agent as a coating" for the conveyor screens. Suitable emulsifying agents include sodium salts ofV sulfonated petroleum hydrocarbons, esters. of sodium sulfosuccinic acid, the sodiumsalt of -sulfonated lauryl alcohol, the sodium salt of a polymerized alkaryl sulfoniczacid,l a mixture of 60% of the sodium salt of water soluble petroleum sulfonate, 25% isopropyl alcohol and 15% water. Oils preferred for use in the emulsions for coating the hot conveyor surfaces are castor oil and corn oil, but others which have been found suitable include other vegetable oils such as" rape seed, cotton seed oil and soy bean oil, fish oils and animal oils such as lard oil. i'

It is important that the particular oil chosen have a low vapor pressure in order to permit its use at dryer temperatures of about 20W-350"7 F. It is preferable that the oil be of a non-drying or semi-drying nature, since drying oils vtend to cause increased fouling of the equipmentv surfaces by the building up of an adherent film or coating. This/tends to increase the frequency or difficulty of cleaning the conveyor screens or other portions of the equipment. In order to reduce the tendency for the oil to undergo undesirable changes, such as polymerization or. sludge deposition, .oilsI .preyiously processed as by hydrogenationor oxidation can be used and known inhibitors yfor oxidation, polymerization or decomposition may be added to the voil. ,.i v

The emulsion is applied to the desired surfaces of the apparatus by brushing, spraying orgb'y other. known means. This: may be accomplished either manually or automatically, for example; by means of applicatorshaving, a: brushing',V Wiping; or rollingactionor byY suitable spray nozzles. In` the'case of continuous operation, as for example using tunnelv type dryers, a preferred methodis to spray the emulsion-l onto the surface of the conveyor during its return pass for example just ahead; of the*V polymer-loading point,l using automatically operated spray nozzles. whoseV motion or delivery is synchronized with the travel ofthe conveyor. The emulsion maybe heated, if desired; to' obtain a suitablefluidity. The quantityh requiredis' relatively small andv isY of courseA dependent upon thetype? of oil chosen, type ofq polymerA being handled, temperature of operation1 and other operating variables. The emulsion has, excellent spreading; qualities which help to-assure'- completecoverage of the surface coated, even thoughthe-quantity'of emulsion used is small. It has been found possible to obtain satisfactory operation in plant" scale tests when using,r no more than 0.5 poundv of: emulsion per 1004 pounds of polymer handled, and'under favorable conditions, an emulsion consumption of about :1 to (L2` pound per 100-pounds of polymer o1: even less can beused.. l

Successful tests have` been conducted using various oils. in the emulsion, but in particular cator oil, and corn-oil have been employed on the conveyor sections of a polymer dryer and have satisfactorily prevented the polymer from sticking tothe-conveyor surfaces. Furthermore, the use of a properly chosen oil does not appreciably affect the propertiesof thefnished polymer since only a portion of the total quantityv of oil used clings to the polymer and appears ultimately in the product. When producing polymers which are"y later to be cured, it is preferable to employ non-drying oilsor to'select oils of relatively low iodineV number, since unsaturated, oils tend to have an undesirable effect on the properties of the cured products. Suitableemulsions useful in this invention` include the following:

3. 40%. blow-n rape seed oil 40%- water 20% emulsifier*' 4. 50% corn oil 37.5% water 12.5% emulsifer* 5; 20%. blown rape seed oil refined rape seed oil 40% water 20% emulsier* Y *A mixture of'60% sodium salt of Watersoluble', petrole"- umsulfonic acids, isopropyl alcohol and 15% water;

The following experiment illustrates the advantages of theV invention:

An emulsion was prepared by mixing in an open-top drum 15 gallons castor oil, 15 gallons Water and 71/2 gallons sodium sulfonate solution consisting ofV 60%- of the sodium salt of Water soluble petroleum sulfonate, 25% isopropyl alcohol and 15% Water. After agitating for one hour, the emulsion waspumped into a lspray gun drum, which was. equipped with an agitator, and

castor oil Water emulsifier* reiinedl rape seedoil water emulsifier" applied to the drier screens of abutyl rubber plant.

No sticking was observed and after a trial of eig-hty days, a considerable reduction in castor oil consumption (approximately 60%) resultedl when the castor oil wasvused in the form of an emulsionI than when it was used straight, as indicated below;

Castor O Consumption For 8 Castor 011 Emulsion consum p. glysEgsl-io Use of Castor tion for lst 8 days oi Test Date on. castor 011 Date Gagstgno l5 30 16 15 17 au 15 22 15 a1 15 15 zu .s 15 4 The'polymer leavingthe dryer or heating zone can be cooled directly for packaging or use; or it can be further processed as by extrusion, compressing,r kneading, milling or sheeting in order to homogenize or compact the polymer, reduce its porosity, or assist the escape of entrapped moisture or other vapors Which may have been formedor-liberated' Within the polymer particles during the heating step.

While one specified process embodying the novel steps of the` present invention, as well as onespecific apparatus for' carrying out-the same has been' described in considerable: detail, it is to be understood that this description is illustrative only, and for the purpose of making the invention more clear', and it is not intended that the invention shall be construed asl limited to detalls of the description except insofar as such limitations have been included in the terms of the following claims in which it is the-intention to claim` allv novelty inherent in the process according to the present invention.

Thenature and objects of the present invention having; been thus described and illustrated, what is claimed as new and useful and is desired to be secured by Letters Patent is:

1. A method of treating solid high molecular weight tacky polymers prepared from mixtures containing substantial amounts of iso-oleus which comprises heating the polymer while passing through. a zone on conveyors the polymercontacting surfaces of which are coated with the. non-volatile residue of a fatty oil emulsion consisting essentially of about 40 to 50% of a fatty oi-l selected` from the group consisting of non-drying and'semi-drying fatty oils, having a low` vapor pressure at 200-350" F., about 121/2 to 20% of an emulsifying agent consisting' essentiallyof a sodium sulfonate, and ther balance of an aqueous* dispersing medium consisting, of at least a.. major proportion of water.

2. A method of drying polymers prepared from mixtures containing substantial amounts of isooleiins, which comprises continuously conveying the polymer through a drying zone on conveyors theconveyor surfaces of which are coated with an emulsion the' non-volatile constituents of which are corn oil and a sodium sulfonate emulsify-ing: agent.

3. A method of drying polymers prepared from mixtures containing substantial amounts of isoclens, which comprises continuously conveying the polymer through a drying zone on conveyors 9 the conveyor surfaces of which are coated with an emulsion the non-volatile constituents of which consist essentially of rape seed oil and a sodium sulfonate emulsifying agent.

4. A method of drying polymers prepared from mixtures containing substantial amounts of isoolens, which comprises continuously conveying the polymer through a drying zone on conveyors the conveyor surfaces oi' which are coated with an emulsion the non-volatile constituents of which consist essentially of castor oil and a sodium sulfonate emulsifying agent. y

5. A method of drying polymers prepared from mixtures containing substantial amounts of isoolens. which comprises continuously conveying the polymer through a drying zone on conveyors the conveyor surfaces of which are coated with an emulsion comprising of 40% castor oil, 40% water and 20% of an emulsiiier comprising 60% of the sodium salt of water-soluble petroleum sulfonic acids, 25% isopropyl alcohol and 15% water.

6. In the process of finishing solid high molecular weight copolymers prepared from mixtures of iso-olens and other unsaturated hydrocarbons at temperatures below about 20 F. in the presence of a Friedel-Crafts type catalyst which comprises discharging the cold polymer and associated low-boiling materials such as unreacted olenic materials, solvents, diluents and the like into water in order to form a slurry of polymer in water and iiash off the bulk of said associated low-boiling materials, stripping said low-boiling materials from the water slurry of polymer, separating the polymer particles` of a fatty oil selected from the group consisting of non-drying and semi-drying fatty oils which are substantially non-volatile at 200-350" F., and emulsifying amount of a sodium 'sulfonate emulsfying agent, and the balance consisting of an aqueous liquid medium comprising atleast l a major proportion of water, the amount of said emulsion used during continuous operation being about 0.1 to 0.5 1b. of the emulsion per 100 lbs. of polymer handled through the dryer. I GRADY R. SCOTT.

REFERENCES CITED The following references are of record in the file of this patent:

UNITEDy STAT-Es PATENTs Number Name Date 539,443 v Proctor May 21, 1895 2,206,046 Pollard July 2, 1940 2,257,167 Gerhardt et al. Sept. 30,1941 2,340,035 Zimmer et al. Jan. l25, 1944k 2,401,754 Green June 11, 1946 2,532,985

Bannon et al. Dec. 5, 1950 

2. A METHOD OF DRYING POLYMERS PREPARED FROM MIXTURES CONTAINING SUBSTANTIALLY AMOUNTS OF ISOOLEFINS, WHICH COMPRISES CONTINUOUSLY CONVEYING THE POLYMER THROUGH A DRYING ZONE ON CONVEYORS THE CONVEYOR SURFACES OF WHCIH ARE COATED WITH AN EMULSION THE NON-VOLATILE CONSTITUENTS OF WHICH ARE CORN OIL AND A SODIUM SULFONATE EMULSIFYING AGENT.
 6. IN THE PROCESS OF FINISHING SOLID HIGH MOLECULAR WEIGHT COPOLYMERS PREPARED FROM MIXTURES OF ISO-OLEIFNS AND OTHER UNSATURATED HYDROCARBONS AT TEMPERATURES BELOW ABOUT -20* F. IN THE PRESENCE OF A FRIEDEL-CRAFTS TYPE CATALYST WHICH COMPRISES DISCHARGING THE COLD POLYMER AND ASSOCIATED LOW-BOILING MATERIALS SUCH AS UNREACTED OLEFINIC MATERIALS, SOLVENTS, DILUENTS AND THE LIKE INTO WATER IN ORDER TO FORM A SLURRY OF POLYMER IN WATER AND FLASH OFF THE BULK OF SAID ASSOCIATED LOW-BOILING MATERIALS, STRIPPING SAID LOW-BOILING MATERIALS FROM THE WATER SLURRY OF POLYMER, SEPARATING THE POLYMER PARTICLES FROM THE WATER SLURRY, PASSING THE SEPARATED POLYMER PARTICLES THROUGH A TUNNEL-TYPE DRYER ON A SCREEN CONVEYOR, PASSING HEATED AIR OVER AND THROUGH A BED OF POLYMER PARTICLES PASSING THROUGH THE DRYER TO REMOVE MOISTURE AND RESIDUAL VOLATILES FROM THE POLYMER, THE IMPROVEMENT CONSISTING IN COATING THE POLYMER-CONTACTING SURFACES OF THE SCREEN CONVEYOR WITH AN EMULSION-CONSISTING ESSENTIALLY OF ABOUT 40 TO 50% OF A FATTY OIL SELECTED FROM THE GROUP CONSISTING OF NON-DRYING AND SEMI-DRYING FATTY OILS WHICH ARE SUBSTANTIALLY NON-VOLATILE AT 200-350* F., AND EMULSIFYING AMOUNT OF A SODIUM SULFONATE EMULSIFYING AGENT, AND THE BALANCE CONSISTING OF AN AQUEOUS LIQUID MEDIUM COMPRISING AT LEAST A MAJOR PROPORTION OF WATER, THE AMOUNT OF SAID EMULSION LUSED DURING CONTINUOUS OPERATION BEING ABOUT 0.1 TO 0.5 LB. OF THE EMULSION PER 100 LBS. OF POLYMER HANDLED THROUGH THE DRYER. 